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CN108027197B - 天然气液化设备液化天然气流的膨胀贮存方法及相关设备 - Google Patents

天然气液化设备液化天然气流的膨胀贮存方法及相关设备 Download PDF

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CN108027197B
CN108027197B CN201680051218.7A CN201680051218A CN108027197B CN 108027197 B CN108027197 B CN 108027197B CN 201680051218 A CN201680051218 A CN 201680051218A CN 108027197 B CN108027197 B CN 108027197B
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natural gas
gas
flash
gaseous
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CN108027197A (zh
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S·沃瓦尔
V·蒂瑞里
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Technip Energies France SAS
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Technip France SAS
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    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F17C9/04—Recovery of thermal energy
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F25J1/0025—Boil-off gases "BOG" from storages
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
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    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
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    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
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    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0219—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. using a deep flash recycle loop
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    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
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Abstract

天然气液化设备液化天然气流的膨胀贮存方法及相关设备。所述方法包括下列步骤：使闪蒸气体气态流(48)与蒸发气体气态流(52)混合，以形成混合气态流(54)；在至少一个压缩装置(30)中压缩混合气态流(54)以形成压缩可燃气流(32)；从压缩可燃气流(32)中提取分流(36)；在至少一个下游压缩机(34)中压缩分流(36)；使压缩分流(66)进行冷却和膨胀；在至少一个下游热交换器(40)中加热从膨胀分流(68)获得的至少第一流(68；70)；在压缩装置(30)的上游，将加热的第一流(68；70)再输入到混合气态流(54)中。

Description

天然气液化设备液化天然气流的膨胀贮存方法及相关设备
技术领域
本发明涉及来自天然气液化设备的液化天然气流的膨胀和贮存方法，其包括下列步骤：
-使液化天然气流在膨胀装置中闪蒸膨胀，以形成膨胀液化天然气流；
-使膨胀液化天然气流进入闪蒸结束贮存器中；
-在闪蒸结束贮存器的底部回收液化天然气液流；
-使液化天然气液流输送到至少一个液化天然气储罐中；
-在闪蒸结束贮存器的顶部提取闪蒸气体气态流；
-在液化天然气储罐的顶部回收蒸发气体气态流；
-使闪蒸气体气态流与蒸发气体气态流混合，以形成混合气态流；
-在至少一个压缩装置中压缩混合气态流，以形成压缩可燃气流。
背景技术
这种方法尤其用于在生产液化天然气的水上液化设备、或者体积小的陆基液化设备中应用。
在目前运转的液化天然气生产厂中，在闪蒸膨胀到大气压之前，天然气在高压下冷凝和过冷。如此获得的液化天然气可在大气压下和在通常约为-160℃的低温下贮存。
膨胀或者直接在液化天然气贮罐处进行，或者在专用单元例如闪蒸气体回收单元中进行。
在这种单元中，膨胀产生的蒸汽予以回收，然后在专用压缩机中压缩以形成可燃气流，或者以在液化系统内再循环。
此外，由于在直接由膨胀获得的液体与贮罐中存在的液体之间的压差，和/或由于液化天然气在向贮罐输送时加热，另一蒸汽流在液化天然气贮罐中产生。
因此，来自贮罐的蒸发气体气态流予以回收，在另一专用压缩机中压缩，以形成可燃气流，或者以在单元内再循环，当单元是水上单元时尤其如此。
这种方法不完全令人满意，尤其是在水上环境中。实际上，所述方法的局限性是需要几个分离的压缩机，通常至少三个压缩机，从而特别笨重庞大，增大了液化设备的固定成本和可变成本。
为了解决这个问题，DE102010062050提出一种方法，其中，闪蒸气体气态流和蒸发气体气态流进行混合，然后在共用压缩机中共同被压缩，以形成可燃气流。
这种方法减小了液化设备的庞大体积，降低了实施成本。但是，所述方法在液化天然气产量和回收方面不完全最佳化。
发明内容
因此，本发明的一目的是获得一种特别紧凑、成本效益特别好的方法，该方法用于通过使用一个或者几个专用于两种功能的压缩机来回收出自天然气液化设备的闪蒸气体和蒸发气体。
为此，本发明涉及一种上述方法，其包括下列步骤：
-从压缩可燃气流中提取分流；
-在至少一个下游压缩机中压缩分流以形成压缩分流；
-冷却压缩分流；
-使压缩分流膨胀以形成膨胀分流；
-在至少一个下游热交换器中加热从膨胀分流获得的至少第一流；
-在压缩装置的上游将加热的第一流再输入到混合气态流中和/或蒸发气体气态流与闪蒸气体气态流的至少一个中。
根据一些具体实施例，根据本发明的方法具有下列一个或多个特征，这些特征可单独考虑或者根据任何技术上可能的组合考虑：
-至少部分呈液态的膨胀分流输入到下游分离瓶中，所述方法还包括下列步骤：
-在下游分离瓶的顶部提取为气体的第一流，使第一流在压缩装置的上游再输入到混合气态流中和/或蒸发气体气态流与闪蒸气体气态流的至少一个中；
-在下游分离瓶的底部回收第二液体分流，在闪蒸结束贮存器的上游使第二液体分流输入到膨胀液化天然气流中；
-整个膨胀分流构成第一流；
-从下游压缩机获得的压缩分流输入到下游热交换器中，以与第一流建立热交换关系；
-蒸发气体气态流输入到下游热交换器中，以与第一流建立热交换关系；
-所述方法还具有下列步骤：
-提供用于被液化的已处理天然气流；
-将已处理天然气流的至少第一部分输入到下游热交换器中，以与第一流建立热交换关系；
-在下游热交换器中通过与第一流的热交换，至少部分地液化已处理天然气流的第一部分；
-所述方法包括在闪蒸结束贮存器的上游，将液化的已处理天然气流的第一部分输入到从膨胀装置获得的膨胀液化天然气流中；
-所述方法还包括下列步骤：
-将已处理天然气流分成已处理天然气流的第一部分和已处理天然气流的第二部分；
-将已处理天然气流的第二部分输入到附加热交换器中，以与闪蒸气体气态流建立热交换关系；
-在附加热交换器中，通过加热闪蒸气体气态流液化已处理天然气流的第二部分；
-在闪蒸结束贮存器的上游，将液化的已处理天然气流的第二部分输入到从膨胀装置获得的膨胀液化天然气流中；
-所述方法还包括下列步骤：
-从压缩分流中分出循环流；
-在下游热交换器中通过与第一流的热交换，液化循环流的至少一部分；
-闪蒸结束贮存器是闪蒸结束分离瓶或者闪蒸结束蒸馏塔；
-膨胀装置具有动态膨胀涡轮；
-已处理天然气流的第一部分的摩尔流量小于从膨胀装置获得的膨胀液化天然气流的摩尔流量的10％。
本发明还涉及一种来自天然气液化设备的液化天然气流的膨胀和贮存设备，膨胀和贮存设备具有：
--膨胀装置，其能进行液化天然气流的闪蒸膨胀，以形成膨胀液化天然气流；
-闪蒸结束贮存器，其能接收来自膨胀装置的膨胀液化天然气流；
-用于在闪蒸结束贮存器的底部回收液化天然气液流的装置；
-至少一个液化天然气贮罐以及用于将液化天然气液流输送到液化天然气贮罐中的装置；
-用于在闪蒸结束贮存器的顶部提取闪蒸气体气态流的装置；
-用于在液化天然气贮罐的顶部回收蒸发气体气态流的装置；
-用于使闪蒸气体气态流与蒸发气体气态流混合以形成混合气态流的装置；
-至少一个压缩装置，其能压缩混合气态流以形成压缩可燃气流；，
其特征在于：
-从压缩可燃气流中提取分流的装置；
-至少一个下游压缩机，用于压缩分流并形成压缩分流；
-下游热交换器，用于冷却压缩分流以形成膨胀分流；
-用于至少部分地使压缩分流膨胀和液化的装置；
-用于使从膨胀分流获得的至少第一流输入到下游热交换器中以能加热第一流的装置；
-用于在压缩装置的上游使加热的第一流再输入到混合气态流中和/或蒸发气体气态流与闪蒸气体气态流的至少一个中的装置。
根据一些具体实施例，根据本发明的设备具有下列一个或多个特征，这些特征可单独考虑或者根据任何技术上可能的组合考虑：
-第一流由整个膨胀分流构成；
-膨胀和贮存设备具有：
-下游分离瓶；
-用于在下游分离瓶的顶部提取为气体的第一流、在压缩装置的上游使第一流再输入到混合气态流中和/或蒸发气体气态流与闪蒸气体气态流的至少一个中的装置；
-用于在下游分离瓶的底部回收第二液体分流、在闪蒸结束分离瓶的上游使第二液体分流输入到膨胀液化天然气流中的装置。
-下游热交换器能与第一流建立热交换关系，已处理天然气流的至少一部分用于液化；
-膨胀和贮存设备具有：
-用于从压缩分流分出循环流的装置；
-用于使循环流的至少一部分输入到下游热交换器中以使该至少一部分至少部分地在下游热交换器中液化的装置。
附图说明
通过阅读下面参照附图仅作为例子给出的说明，本发明将得到更好理解，附图中：
图1是用于实施根据本发明的第一种方法的第一液化设备的框图；
图2至6是用于实施根据本发明的变型方法的替换液化设备的框图。
具体实施方式
下文中，相同的标号将用于标示在管道中流通的气流及输送气流的所述管道。此外，术语“上游”和“下游”一般理解为相对于流体的正常流向而言的。
此外，除非另有陈述，百分比是摩尔百分率，压力以绝对巴给出。
所描述的附加涡轮驱动压缩机，但是也可驱动变频发电机，发电机所发的电可通过变频器用于电网中。
温度高于环境温度的气流描述为其由空气冷却器冷却。可替换地，可以使用例如用淡水或者海水的水交换器。
对于本发明来说，液化设备周围的环境温度不高，尤其可为15℃至35℃之间。
用于使由天然气液化设备12获得的液化天然气流进行膨胀和贮存的第一液化设备10示意地示于图1。
有利地，液化设备10、12由支承件14承载，所述支承件14位于如大海、湖泊、海洋或者河流这样的水域的表面上。例如，支承件14是浮船，构成水上天然气液化单元。
这里，液化设备12不予详述。在已知方式中，其具有天然气处理单元16和已处理气体液化单元18，天然气处理单元16能产生没有在液化期间可能固结的成分的已处理气体，已处理气体液化单元18具有至少一个用于已处理气体20冷却、液化和过冷的系统(未示出)，其能产生增压液化天然气流22。
膨胀和贮存设备10具有增压液化天然气流22的膨胀装置24，这里，膨胀装置具有动态膨胀涡轮25和闪蒸结束贮存器，在该具体实施例中，闪蒸结束贮存器为闪蒸结束分离瓶26。其也具有至少一个液化天然气回收贮罐28和压缩装置30，它们能回收和压缩来自贮存器26的闪蒸气体和来自所述一个或者每个贮罐28的蒸发气两者，以形成压缩可燃气流32。
根据本发明，设备10还具有下游压缩机34和至少一个动态膨胀涡轮38，所述下游压缩机34用于压缩从压缩可燃气流32中提取的分流36，所述至少一个动态膨胀涡轮38能使分流36膨胀。
在图1所示的实施例中，设备10还具有下游热交换器40和附加热交换器41，它们用于利用分流36在涡轮38中进行动态膨胀期间产生的冷量，来液化至少一部分已处理气体20。
可替换地或者附加地，如图3中下面所述，交换器40和41用于当压缩可燃气流32中存在过量闪蒸气体和/或蒸发气体时，至少部分地冷却和液化分流36的一部分。
现在来说明根据本发明的用于在设备10中应用的液化天然气流22膨胀和贮存的第一种方法。
最初，增压液化天然气流22由设备12产生。
液化天然气流22的压力例如超过60巴，可为40巴至80巴之间。
气流22是过冷气流。液化天然气流22的温度通常低于-150℃，但是可在-140℃至-160℃之间。
有利地，气流22的甲烷摩尔含量大于80％，C4 +摩尔含量低于5％。
液化天然气流22的摩尔流量例如大于10000千摩尔/小时。
液化天然气流22被输送到膨胀装置24的动态膨胀涡轮25，以在其中进行闪蒸膨胀并形成膨胀液化天然气流42。
膨胀液化天然气流42的压力例如低于7巴，尤其是在6巴至12巴之间。
气流22的膨胀致使残余闪蒸气体在最终膨胀阀的下游形成于气流42中。气流42中的闪蒸气体的摩尔含量例如大于5％，尤其是在4％至10％之间。
然后，气流42被输入到闪蒸结束分离瓶26中，以在分离瓶26的底部回收液化天然气液流46，而在分离瓶26的顶部回收闪蒸气体气态流48。
然后，液流46向贮罐28输送。在图1所示的实施例中，液流46通过泵50泵送。可替换地，液流在重力作用下流入贮罐28，无需泵送。
在其输送和输入到贮罐28中的期间，尤其是通过液流46在输送管道中加热、通过贮罐28吸热和/或在分离瓶26与贮罐28之间的压差作用下，残余蒸发气体从液流46形成。
蒸发气体气态流52在贮罐28的顶部进行回收。蒸发气体气态流52在下游膨胀器40中被加热到例如高于-60℃的温度。
闪蒸气体气态流48在附加膨胀器41中被加热到例如高于-60℃的温度。
然后，闪蒸气体气态流与蒸发气体气态流52混合，以形成混合气态流54。
气态流48占混合气态流54的30mol％(摩尔百分比)至80mol％。
然后，混合气态流54输入到压缩装置30中，以形成压缩可燃气流32。
在图1所示的实施例中，气流54相继经过第一压缩机56、第一气冷交换器或者水交换器58以被冷却到环境温度、第二压缩机60、然后是第二交换器62以重新被冷却到环境温度或者水温。
压缩可燃气流32的压力例如高于25巴，尤其是在5巴至70巴之间。
在一具体实施例中，气流32的成分由通常15mol％的氮和85mol％的甲烷组成。
然后，压缩可燃气流32予以回收，以用作设备12中的燃料或者作为设备12中的备用流体。
分流36在可燃气流32中提取。分流36的摩尔流量例如大于从压缩装置30获得的可燃气流32的摩尔流量的10％，尤其是在该流量的10％至100％之间。
然后，分流36在压缩机34中压缩，然后在气冷交换器或者水交换器64中被冷却到环境温度，以形成一压缩分流66。
压缩分流66的压力例如比气流32的压力高30巴。
然后，压缩分流66输入到下游热交换器40中，以在其中过冷到有利地低于-50℃的温度。
然后，其在动态膨胀涡轮38中膨胀到低于2巴的压力，尤其是在1.1巴至3巴之间，以形成膨胀分流68。
膨胀分流68的温度优选低于-150℃，尤其是在-140℃至-160℃之间。
膨胀分流68可选地至少部分地为液体。在这种情况下，膨胀分流68中液体的摩尔含量通常低于15mol％。可替换地，膨胀分流68完全保持气态。
在该实施例中，整个膨胀分流68形成第一流70，第一流然后输入到下游热交换器40中，以在其中被加热。加热的第一流71的温度有利地高于-60℃。
然后，加热的第一流71在闪蒸结束分离瓶26的下游和压缩装置30的上游，再输入到混合流54中。
在该实施例中，从设备12获得的至少一个已处理气体气态流72引向设备10。
气态流72的压力例如超过60巴，尤其是在40巴至90巴之间。该气态流的温度通常等于环境温度或者预冷却温度。
气态流72的甲烷摩尔含量高于80％，C4 +摩尔含量低于5％。
气态流72的摩尔流量可高达输入到液化设备12中的初始天然气负荷的流量的10％。
然后，气态流72分成第一部分74和第二部分76。
气态流72的第一部分74的摩尔流量例如构成气态流72的20mol％至50mol％之间，气态流72的第二部分76的摩尔流量例如构成气态流72的摩尔流量的50％至80％之间。
然后，气态流72的第一部分74输入到下游热交换器40中，以在其中通过尤其与膨胀分流68的热交换，被冷却和液化到有利地低于-150℃的温度。
然后，第一部分74经过控制阀78，再与从膨胀装置24获得的膨胀液化天然气流42混合。
气态流72的第二部分76输入到附加热交换器41中，以在其中通过与闪蒸气体气态流48的热交换，被冷却和液化到有利地低于-150℃的温度。
然后，第二部分76经过控制阀80，再与从膨胀装置24获得的膨胀液化天然气流42混合。
因此，根据本发明的方法实施起来特别简单，因为其减少了进行液化天然气闪蒸以贮存液化天然气、和有利地回收产生的闪蒸气体和蒸发气体所需的设备部件的数量。
特别是，单一压缩装置30用于压缩由闪蒸气体和蒸发气体形成的混合流54。
从在压缩装置30的出口形成的可燃气流32中提取的分流36的利用，允许获得非常有效的热综合利用，受益于可用来至少部分地液化所述设备12中处理过的气体的冷量。
分流36的热综合利用允许调节设备10的不同运行方式之间、储瓶装填阶段与甲烷贮存罐装载阶段之间的冷量。
因此，根据本发明的方法及可实施这种方法的设备10特别适于水上装置，例如水上天然气液化设备FLNG。
在图1示意地示出的一变型中，蒸发气体气态流的一部分90被送向其他液化系统。相反，来自其他液化系统的液化天然气流92输入到贮罐28中。
根据本发明的第二种设备110示于图2。第二种设备110与第一种设备10的不同之处在于，其具有布置在动态膨胀涡轮38的出口的下游分离瓶112。
膨胀分流68输入到下游分离瓶112中，以在顶部回收呈气态形式的第一流70，而在底部回收第二液流114。
第二液流114的摩尔流量例如构成膨胀分流68的摩尔流量的10％至15％之间。
如以前一样，第一流70输入到下游热交换器40中，以通过尤其与已处理气体气态流72的第一部分74的热交换而被加热。
第二液流114在闪蒸结束分离瓶26的上游再输入到从膨胀装置24获得的膨胀液化天然气流42中。
根据本发明的第二种方法使下游热交换器40中液体的分配最佳化。
用于实施根据本发明的第三种方法的第三种设备120示于图3。
与图1所示设备10中实施的第一种方法不同的是，从压缩分流66中提取出循环流122。
循环流122例如占从压缩机34获得的压缩分流66的30％至80％之间。
然后，循环流122分成第一部分124和第二部分126。
循环流122的第一部分124的摩尔流量例如构成循环流122的20mol％至50mol％之间，循环流122的第二部分126的摩尔流量例如构成循环流122的摩尔流量的50％至80％之间。
循环流122的第一部分124输入到下游热交换器40中，以在其中通过尤其与膨胀分流68的热交换，被冷却到有利地低于-150℃的温度和可选地至少部分地被液化。
然后，第一部分124经过控制阀128，再与从膨胀装置24获得的膨胀液化天然气流42混合。
分流122的第二部分126输入到附加热交换器41中，以在其中通过与闪蒸气体气态流48的热交换，被冷却到有利地低于-150℃的温度和可选地至少部分地液化。
然后，第二部分126经过控制阀130，再与从膨胀装置24获得的膨胀液化天然气流42混合。
在产生过量闪蒸气体和/或蒸发气体时，从在压缩装置30的出口形成的可燃气流32中提取的分流36的利用可获得非常有效的热综合利用，受益于可用于至少部分地液化从分流获得的循环流122的冷量。
在图3虚线所示的变型中，从设备12获得的已处理气体气态流72的至少一部分76也输入到附加热交换器41中，如上面对于图2所描述的。
用于实施根据本发明的第四种方法的第四种设备130示于图4。
该设备130与图1所示设备10的不同之处在于，闪蒸结束分离瓶26被闪蒸结束蒸馏塔132取代。
再沸交换器134定位在膨胀装置24的上游，以使液化天然气流22与从蒸馏塔132获得的再沸流136建立热交换关系。
根据本发明的第四种方法的实施也类似于根据本发明的第一种方法的实施。
用于实施根据本发明的第五种方法的第五种设备140示于图5。
该设备140与图3所示设备120的不同之处在于，闪蒸结束分离瓶26被闪蒸结束蒸馏塔132取代。
根据本发明的第五种方法的实施也类似于根据本发明的第三种方法的实施。
用于实施根据本发明的第六种方法的第六种设备150示于图6。
第六种设备150与第四种设备130的不同之处在于，在膨胀装置24的出口与蒸馏塔132的入口之间插入中间瓶152。
中间瓶152接纳膨胀液化天然气流42，使之在到达蒸馏塔132之前，分成与闪蒸气体气态流48混合的顶部气流154和输入到再沸交换器134中的底部气流156。
在顶部气流154富含氦、通常含至少25％的氦、因此可有利地被送入氦净化设备中的情况下，该设备150有利于回收氦。
在每一种设备120至150的变型中，提供下游瓶112以像根据本发明的第二种方法中所描述的那样，分开膨胀分流68。
在上述设备的一变型中，膨胀装置24的动态膨胀涡轮25被静态膨胀阀代替。然后，液化天然气流在膨胀装置24中进行静态、而不是动态的膨胀。
因此，根据本发明的方法和相应的设备特别适于在通过排空贮罐的甲烷船装载阶段与贮罐装填阶段之间，管控来自贮罐28的蒸发气体气态流52的很大的温度和流量变化。
如上所述，分流36与蒸发气体气态流52的热综合利用，用于调节必要的冷量以及改变可燃气流32和分流36的相对流量。
特别是在主要液化周期，无需改变天然气液化的操作参数，即可达此目的。

Claims (15)

1.一种用于膨胀和贮存来自天然气液化设备(12)的液化天然气流(22)的方法，所述方法包括下列步骤：
-使液化天然气流(22)在膨胀装置(24)中闪蒸膨胀，以形成膨胀液化天然气流(42)；
-使膨胀液化天然气流(42)进入闪蒸结束贮存器中；
-在闪蒸结束贮存器的底部回收液化天然气液流(46)；
-使液化天然气液流(46)输送到至少一个液化天然气储罐(28)中；
-在闪蒸结束贮存器的顶部提取闪蒸气体气态流(48)；
-在液化天然气储罐(28)的顶部回收蒸发气体气态流(52)；
-使闪蒸气体气态流(48)与蒸发气体气态流(52)混合，以形成混合气态流(54)；
-在至少一个压缩装置(30)中压缩混合气态流(54)，以形成压缩可燃气流(32)；
所述方法的特征在于下列步骤：
-从压缩可燃气流(32)中提取分流(36)；
-在至少一个下游压缩机(34)中压缩分流(36)以形成压缩分流(66)；
-冷却压缩分流(66)；
-使压缩分流(66)膨胀以形成膨胀分流(68)；
-在至少一个下游热交换器(40)中加热从膨胀分流(68)获得的至少第一流(70)；
-在压缩装置(30)的上游将加热的第一流再输入到混合气态流(54)中和/或蒸发气体气态流(52)与闪蒸气体气态流(48)的至少一个中；
蒸发气体气态流(52)输入到下游热交换器(40)中，以与第一流(70)建立热交换关系，并且
压缩可燃气流予以回收，用作天然气液化设备中的燃料或者作为天然气液化设备中的备用流体。
2.根据权利要求1所述的方法，其特征在于，至少部分呈液态的膨胀分流(68)输入到下游分离瓶(112)中，所述方法还包括下列步骤：
-在下游分离瓶(112)的顶部提取为气体的第一流(70)，使第一流(70)在压缩装置(30)的上游再输入到混合气态流(54)中和/或蒸发气体气态流(52)与闪蒸气体气态流(48)的至少一个中；
-在下游分离瓶(112)的底部回收第二液体分流(114)，在闪蒸结束贮存器的上游使第二液体分流(114)输入到膨胀液化天然气流(42)中。
3.根据权利要求1所述的方法，其特征在于，整个膨胀分流(68)构成第一流(70)。
4.根据权利要求1或2所述的方法，其特征在于，从下游压缩机(34)获得的压缩分流(66)输入到下游热交换器(40)中，以与第一流(70)建立热交换关系。
5.根据权利要求1或2所述的方法，其特征在于，所述方法还具有下列步骤：
-提供用于被液化的已处理天然气流(72)；
-将已处理天然气流(72)的至少第一部分(74)输入到下游热交换器(40)中，以与第一流(70)建立热交换关系；
-在下游热交换器(40)中通过与第一流(70)的热交换，至少部分地液化已处理天然气流(72)的第一部分(74)。
6.根据权利要求5所述的方法，其特征在于，所述方法包括在闪蒸结束贮存器的上游，将液化的已处理天然气流(72)的第一部分(74)输入到从膨胀装置(24)获得的膨胀液化天然气流(42)中。
7.根据权利要求5所述的方法，其特征在于，所述方法还包括下列步骤：
-将已处理天然气流分成已处理天然气流(72)的第一部分(74)和已处理天然气流(72)的第二部分(76)；
-将已处理天然气流(72)的第二部分(76)输入到附加热交换器(41)中，以与闪蒸气体气态流(48)建立热交换关系；
-在附加热交换器(41)中，通过加热闪蒸气体气态流(48)液化已处理天然气流(72)的第二部分(76)；
-在闪蒸结束贮存器的上游，将液化的已处理天然气流(72)的第二部分(76)输入到从膨胀装置(24)获得的膨胀液化天然气流(42)中。
8.根据权利要求1或2所述的方法，其特征在于，所述方法还包括下列步骤：
-从压缩分流(66)中分出循环流(122)；
-在下游热交换器(40)中通过与第一流(70)的热交换，液化循环流(122)的至少一部分(124)。
9.根据权利要求1或2所述的方法，其特征在于，闪蒸结束贮存器是闪蒸结束分离瓶(26)或者是闪蒸结束蒸馏塔(132)。
10.根据权利要求1或2所述的方法，其特征在于，膨胀装置(24)具有动态膨胀涡轮(25)。
11.一种来自天然气液化设备(12)的液化天然气流的膨胀和贮存设备，膨胀和贮存设备具有：
-膨胀装置(24)，其能进行液化天然气流(22)的闪蒸膨胀，以形成膨胀液化天然气流(42)；
-闪蒸结束贮存器，其能接收来自膨胀装置(24)的膨胀液化天然气流(42)；
-用于在闪蒸结束贮存器的底部回收液化天然气液流(46)的装置；
-至少一个液化天然气贮罐(28)以及用于将液化天然气液流(46)输送到液化天然气贮罐(28)中的装置；
-用于在闪蒸结束贮存器的顶部提取闪蒸气体气态流(48)的装置；
-用于在液化天然气贮罐(28)的顶部回收蒸发气体气态流(52)的装置；
-用于使闪蒸气体气态流(48)与蒸发气体气态流(52)混合以形成混合气态流(54)的装置；
-至少一个压缩装置(30)，其能压缩混合气态流(54)以形成压缩可燃气流(32)；
其特征在于：
-从压缩可燃气流(32)中提取分流(36)的装置；
-至少一个下游压缩机(34)，用于压缩分流(36)并形成压缩分流(66)；
-下游热交换器(40)，用于冷却压缩分流(66)以形成膨胀分流(68)；
-用于至少部分地使压缩分流(66)膨胀和液化的装置；
-用于使从膨胀分流(68)获得的至少第一流(70)输入到下游热交换器(40)中以能加热第一流(70)的装置；
-用于在压缩装置(30)的上游使第一流(70)再输入到混合气态流(54)中和/或蒸发气体气态流(52)与闪蒸气体气态流(48)的至少一个中的装置；
-用于蒸发气体气态流(52)输入到下游热交换器(40)中以与第一流(70)建立热交换关系的装置，并且
压缩可燃气流予以回收，用作天然气液化设备中的燃料或者作为天然气液化设备中的备用流体。
12.根据权利要求11所述的膨胀和贮存设备，其特征在于，第一流(70)由整个膨胀分流(68)构成。
13.根据权利要求11所述的膨胀和贮存设备，其特征在于，膨胀和贮存设备具有：
-下游分离瓶(112)；
-用于在下游分离瓶(112)的顶部提取为气体的第一流(70)、在压缩装置(30)的上游使第一流(70)再输入到混合气态流(54)中和/或蒸发气体气态流(52)与闪蒸气体气态流(48)的至少一个中的装置；
-用于在下游分离瓶(112)的底部回收第二液体分流(114)、在闪蒸结束贮存器的上游使第二液体分流(114)输入到膨胀液化天然气流(42)中的装置。
14.根据权利要求11至12中任一项所述的膨胀和贮存设备，其特征在于，下游热交换器(40)能与第一流(70)建立热交换关系，已处理天然气流(72)的至少一部分(74)用于液化。
15.根据权利要求11至12中任一项所述的膨胀和贮存设备，其特征在于，膨胀和贮存设备具有：
-用于从压缩分流(66)分出循环流(122)的装置；
-用于使循环流(122)的至少一部分(124)输入到下游热交换器(40)中以使该至少一部分至少部分地在下游热交换器(40)中液化的装置。
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